NAPHTHALENE ALKYLATION PROCESS USING MIXED H/NH3 FORM CATALYST

Abstract: Long chain alkyl substituted naphthalenes are produced by alkylating naphthalene with an olefin or other alkylating agent with at least 6, and usually 12 to 20 carbon atoms, in the presence of an alkylation catalyst comprising a zeolite having both ammonium and protonic species associated with the exchangeable sites of the zeolite. The zeolite is usually a large pore size zeolite such as USY. The presence of both ammonium and protonic species increases selectivity for production of long chain mono-alkyl substituted naphthalenes in preference to more highly substituted products.

Description: Naphthalene Alkylation Process Using Mixed H/NH3 Form Catalyst This invention relates to the production of alkylated naphthalenes and substituted naphthalenes. Alkylaromatic fluids have been proposed for use as certain types of functional fluids where good thermal and oxidative are required. For example, U.S. Patent No. 4,714,794 (Yoshida) describes the monoalkylated naphthalenes as having excellent thermal and oxidative stability, low vapor pressure and flash point, good fluidity and high heat transfer capacity and other properties which render them suitable for use as thermal medium oils. The use of a mixture of monoalkylated and polyalkylated naphthalenes as a base for synthetic functional fluids is described in U.S. Patent no. 4,604,491 (Dressier) and Pellegrini U.S. 4,211,665 and 4,238,343 describe the use of alkylaromatics as transformer oils. The alkylated naphthalenes are usually produced by the alkylation of naphthalene or a substituted naphthalene in the presence of an acidic alkylation catalyst such as a Friedel-Crafts catalyst, for example, an acidic clay as described in Yoshida U.S. 4,714,794 or Dressier U.S. 4,604,491 or a Lewis acid such as aluminum trichloride as described in Pellegrini U.S. 4,211,665 and 4,238,343. The use of a catalyst described as a collapsed silica-alumina zeolite as the catalyst for the alkylation of aromatics such as naphthalene is disclosed in Boucher U.S. 4,570,027. The use of various zeolites including intermediate pore size zeolites such as ZSM-5 and large pore size zeolites such as zeolite L and ZSM-4 for the alkylation of various monocyclic aromaticε such as benzene is disclosed in Young U.S. 4,301,316. In the formulation of functional fluids based on the alkyl naphthalenes, it has been found that the preferred alkyl naphthalenes are the mono-substituted naphthalene since they provide the best combination of properties in the finished product: because the mono-alkylated naphthalenes possess fewer benzylic hydrogens than the corresponding di-substituted or polysubstituted versions, they have better oxidative stability and therefore form better functional fluids and additives. In addition, the mono-substituted naphthalenes have a kinematic viscosity in the desirable range of 5-8 mm 2 /s (at 100°C.) when working with alkyl substituents of 14 to 18 carbon atoms chain length. Although the mono-alkylated naphthalenes may be obtained in admixture with more highly alkylated naphthalenes using conventional Friedel-Crafts catalysts such as those mentioned above or by the use of zeolites such as USY, the selectivity to the desired mono-alkylated naphthalenes is not as high as desired. Several recent advances have been made in this area which improve the yields of the desired mono-alkylated naphthenes. U.S. 5,034,563, Ashjian et al, teaches use of a zeolite containing a bulky cation. The use of, e.g., USY with cations having a radius of at least 25 nm (2.5 Angstroms) increases selectivity for desired products. Taught as suitable were zeolites containing hydrated cations of metals of Group IA, divalent cations, especially of Group IIA, and cations of the Rare Earths. The patent had examples in which H, NH4, Na were added to USY zeolite by a procedure involving forming a slurry of zeolite and liquid, 1 hour of stirring, decantation, and a repeat of the exchange procedure. U.S. 5,177,284, Le et al, discusses the desirable properties of alkylated naphthalene fluids with higher alpha:beta ratios, including improved thermal and oxidative stability. Le et al found that several parameters influenced the alpha:beta ratio of the alkylated naphthalene products, including steaming the zeolite, lowering the alkylation temperature, or use of acid-treated clay. Steamed USY catalyst gave excellent results in the examples. The patentees also mentioned use of zeolites with reduced activity due to base exchange, alkaline earth ion exchange and use of boron-zeolite beta. U.S. 5,191,135 Dwyer et al, discloses the effect of co-feeding water for this reaction when using a large pore zeolite catalyst, such as zeolite Y. Adding from 1 - 3 wt % water to the feed improved the alkylation reaction, a result attributed to suppression of zeolite acid site activity. U.S. 5,191,134, Le, discloses a similar alkylation process using MCM-41. The present inventors did additional work to see if this alkylation process can be approved. They wanted to increase the efficiency of the reaction both in terms of conversion and yields. It was found that catalyst containing a roughly 50/50 (molar basis) of NH4 and H gave unexpectedly superior results. Phrased another way, catalyst which was exchanged with ammonia, and then only about half calcined, gave better results than catalyst which was wholly in the ammonium form, or calcined to be in the protonic form. Although the performance of the catalyst could be improved by the incorporation of rare earths, excellent catalyst with essentially no rare earths present can be prepared. Accordingly, the present invention provides a process for preparing long chain alkyl substituted naphthalenes which comprises alkylating a naphthalene with an alkylating agent possessing an alkylating aliphatic group having at least six carbon atoms under alkylation reaction conditions in the presence of an alkylation catalyst comprising a porous crystalline zeolite containing exchangeable sites and both ammonium and protonic species associated with the exchangeable sites, and wherein the ratio of ammonium:protonic species is within the range of 95:5 to 5:95, molar basis, to form an alkylated naphthalene possessing at least one alkyl group derived from the alkylating agent. In another embodiment, the present invention provides a process for preparing long chain alkyl substituted naphthalenes which comprises reacting naphthalene with an olefin containing at least 8 carbon atoms as an alkylating agent under alkylation reaction conditions and in the presence of an alkylation catalyst comprising an ultrastable Y zeolite with exchangeable sites containing both ammonium and protonic species associated with the exchangeable sites, and wherein the molar ratio of ammonium:protonic species is from 65:35 to 35:65 to form an alkylated naphthalene possessing at least one alkyl group derived from the alkylating agent. The starting materials for the production of the alkylated naphthalenes are naphthalene itself as well the substituted naphthalenes which may contain one or more short chain alkyl groups containing up to eight carbon atoms, such as methyl, ethyl or propyl. Suitable alkyl- substituted naphthalenes include alpha-methylnaphthalene, dimethylnaphthalene and ethylnaphthalene. Naphthalene itself is preferred since the resulting mono-alkylated products have better thermal and oxidative stability than the more highly alkylated materials for the reasons set out above. The alkylating agents which are used to alkylate the naphthalene include any aliphatic or aromatic organic compound having one or more available alkylating aliphatic groups capable of alkylating the naphthalene. The alkylatable group itself should have at least 6 carbon atoms, preferably at least 8, and still more preferably at least 12 carbon atoms. For the production of functional fluids and additives, the alkyl groups on the alkyl- naphthalene preferably have from 12 to 30 carbon atoms, with particular preference to 14 to 18 carbon atoms. A preferred class of alkylating agents are the olefins with the requisite number of carbon atoms, for example, the hexenes, heptenes, octenes, nonenes, decenes, undecenes, dodecenes. Mixtures of the olefins, e.g. mixtures of C 12 - C 20 or C 14 -C 18 olefins, are useful. Branched alkylating agents, especially oligomerized olefins such as the trimers, tetramers, pentamers, etc., of light olefins such as ethylene, propylene, the butylenes, etc. , are also useful. Other useful alkylating agents which may be used, although less easily,- include alcohols (inclusive of monoalcohols, dialcohols, trialcohols, etc.) such as hexanols, heptanols, octanols, nonanols, decanols, undecanols and dodecanols; and alkyl halides such as hexyl chlorides, octyl chlorides, dodecyl chlorides; and higher homologs. The alkylation reaction between the naphthalene and the alkylating agent is carried out in the presence of a zeolite catalyst which contains a cation of certain specified radius. The molecular size of the alkylation products will require a relatively large pore size in the zeolite in order for the products to leave the zeolite, indicating the need for a relatively large pore size in the zeolite, which will also tend to reduce diffusion limitations with the long chain alkylating agents. The large pore size zeolites are the most useful zeolite catalysts for this purpose although the less highly constrained intermediate pore size zeolites may also be used, as discussed below. The large pore size zeolites are zeolites such as faujasite, the synthetic faujasites (zeolites X and Y) , zeolite L, ZSM-4, ZSM-18, ZSM-20, mordenite and offretite which are generally useful for this purpose are characterized by the presence of a 12-membered oxygen ring system in the molecular structure and by the existence of pores with a minimum dimension of at least 74 nm (7.4 A), as described by Frilette et al. in J. Catalysis e>2,218-222 (1981) . See also Chen et al. Shape-Selective Catalysis in Industrial Applications. (Chemical industries; Vol. 36) Marcel Dekker Inc., New York 1989, ISBN 0-8247- 7856-1 and Hoelderich et al. Anqew. Chem. Int. Ed. Enql. 27 226-246 (1988), especially pp.226-229. The large pore size zeolites may also be characterized by a "Constraint Index" of not more than 2, in most cases not more than 1. Zeolite beta, a zeolite having a structure characterized by twelve- membered pore openings, is included in this class of zeolites although under certain circumstances it has a Constraint Index approaching the upper limit of 2 which is characteristic of this class of zeolites. The method for determining Constraint Index is described in U. S. Patent No. 4,016,218, together with values for typical zeolites and of the significance of the Index in U.S. Patent No.4,861,932, to which reference is made for a description of the test procedure and its interpretation. Zeolites whose structure is that of a ten membered oxygen ring, generally regarded as the intermediate pore size zeolites may also be effective catalysts for this alkylation reaction if their structure is not too highly constrained. Thus, zeolites such as ZSM-12 (Constraint Index 2) may be effective catalysts for this reaction. The zeolite identified as MCM-22 is a useful catalyst for this reaction. MCM-22 is described in U.S. Patent 4,954,325, to which reference is made for a description of this zeolite. Thus, zeolites having a CI up to about 3 will generally be useful catalysts, although the activity may be found to be dependent on the choice of alkylating agent, especially its chain length, a factor which imposes diffusion limitations upon the choice of zeolite. A highly useful zeolite for the production of the mono-alkylated naphthalenes is ultrastable Y, usually referred to as USY. When this material contains hydrated cations, it catalyses the alkylation in good yields with excellent selectivity. Zeolite USY is a material of commerce, available in large quantities as a catalyst for the cracking of petroleum. It is produced by the stabilization of zeolite Y by a procedure of repeated ammonium exchange and controlled steaming. Processes for the production of zeolite USY are described in U. S. Patents Nos. 3,402,966 (McDaniel) , 3,923,192 (Maher) and 3,449,070 (McDaniel) ; see also Wojciechowski, Catalytic Cracking. Catalysts, Chemistry and Kinetics. (Chemical Industries Vol. 25) , Marcel Dekker, New York, 1986, ISBN 0- 8247-7503-8, to which reference is made for a description of zeolite USY, its preparation and properties. Small crystal Y zeolite, in the 0.2 to 0.4 μm range is preferred, although the 0.6 to 1.3 μm material which is more typical of Y zeolite crystals may also be used. It is essential to put the zeolite in a form in which the cation exchange sites contain both ammonium and protonic species. Expressed as % of total ion exchange capacity, the zeolite should contain at least 35 % ammonium and at least 35 % protonic forms. Preferably, the ammonium and protonic forms each occupy at least 40 % of the available sites. Most preferably the ammonium form is 55 to 50 % of the available sites, with the protonic form being the remainder. As used herein, the total ion exchange capacity of the catalyst may be determined by the temperature programmed ammonia desorption method described by G. T. Kerr and A. W. Chester in Thermochimica Acta, 3 . , 113-124 (1971) . This ratio of ammonium to protonic forms, may also be expressed in terms of a standardized calcination procedure after ammonium exchange. Thus the zeolite may be placed in the ammonium form using conventional techniques. Typically this involves contacting the zeolite, or catalyst, with 5 vol/vol of 1 N NH4N03 and stirring for an hour, water washing, another exchange step, and a final wash. The catalyst then may be calcined for 5 hours in flowing air. When this procedure is used, calcining at 400 - 425°C gives optimum results. The above ratios, of ammonium to protonic forms, hold even if other ions are present. Thus the presence of Rare Earths, discussed below, may reduce the total amount of ammonium and protonic ions present, but will not alter the critical ratio of ammonium:protonic species. RARE EARTH EXCHANGE The selected zeolite catalyst preferably contains a limited amount of one or more of the Rare Earths. Suitable are Y, La and any of the Lanthanum Series of Rare Earths, Ce, Pr, Nd, Pm, Sm, Eu, Gd, Tb, Dy, Ho, Er, Tm Yb, and Lu. Especially preferred are Ce, Y and La. In most applications, mixtures of rare earths will be preferred, as these are readily available commercially and much less expensive than purified rare earth elements. The mixed rare earths typically used to produce zeolite Y based cracking catalysts serve well. If the zeolite does not contain the desired amount of rare earths they may be introduced by ion-exchange in the conventional manner using a solution of the exchanging cation. It is preferred to have less than 50 % of the total number of exchangeable sites associated with Rare Earths. Preferably less than 35 % of the exchangeable sites contain Rare Earths, and most preferably less than about 20 % exchange is preferred. Optimum results are seen with 12.5 to 17.5 % Rare Earth exchange, ideally, with about 15 % exchange. For a typical catalyst, comprising 40 wt % USY zeolite in a conventional binder or matrix as discussed below, the optimum RE content will be about 1 wt %, equivalent to a rare earth content corresponding to less than about 15 % of the total number of exchangeable sites. Binders may be used to improve crush strength and other physical properties. Suitable materials include naturally occurring clays, e.g., bentonite and kaolin as well as silica, alumina, and mixtures thereof. The relative proportions of zeolite, present in finely divided crystalline form, and oxide matrix may vary widely, with the crystalline zeolite content ranging from 1 to 90 percent by weight and more usually, particularly when the composite is prepared in the form of beads, in the range of 2 to 80 weight percent of the composite. The stability of the alkylation catalyst of the invention may be increased by steaming. U.S. Patent Nos. 4,663,492; 4,594,146; 4,522,929; and 4,429,176, describe conditions for the steam stabilization of zeolite catalysts which can be utilized to steam-stabilize the catalyst. Care should be taken to ensure that steaming conditions are not so severe as to convert too much of the ammonium species to protonic species. The alkylation process of this invention is conducted such that the organic reactants, i.e., the alkylatable aromatic compound and the alkylating agent, are brought into contact with the zeolite catalyst in a suitable reaction zone such as, for example, in a flow reactor containing a fixed bed of the catalyst composition, under effective alkylation conditions. Such conditions typically include a temperature of from 100°C to 400°C, a pressure of from 20.3 to 25325 kPa (0.2 to 250 atmospheres) , a feed weight hourly space velocity (WHSV) of from 0.1 hr "1 to 10 hr "1 and an alkylatable aromatic compound to alkylating agent mole ratio of from 0.1:1 to 50:1, preferably from 4:1 to 1:4 e.g. from 2:1 to 1:2. The WHSV is based upon the weight of the catalyst composition employed, i.e., the total weight of active catalyst (and binder if present) . Preferred reaction conditions include a temperature within the approximate range of from 100°C to 350°C, a pressure of from 101 to 2533 kPa (1 to 25 atmospheres) , a WHSV of from 0.5 hr -1 to 5 hr "1 and an alkylatable aromatic compound to alkylating agent mole ratio of from 0.5:1 to 5:1. When using naphthalene as the aromatic compound, the pressure should preferably be maintained at a value of at least 448 kPa abs (50 psig) in order to prevent the naphthalene from subliming into the overhead of the alkylation reactor; the required pressure may be maintained by inert gas pressurization, preferably with nitrogen. The reactants can be in either the vapor phase or the liquid phase and can be neat, i.e., free from intentional admixture or dilution with other material, or they can be brought into contact with the zeolite catalyst composition with the aid of carrier gases or diluents such as, for example, hydrogen or nitrogen. The alkylation can be carried out as a batch- type reaction typically employing a closed, pressurized, stirred reactor with an inert gas blanketing system or in a semi-continuous or continuous operation utilizing a fixed or moving bed catalyst system. The presence of some water may improve selectivity, e.g., operation with water addition to the feed or hydration of the catalyst. For a fluid bed reactor operation with about 0.75 wt % water in the reaction mixture is preferred. The products comprising alkylated aromatics are characterized by exceptional oxidative and thermal stability. They may be separated from the reaction mixture by stripping off unreacted alkylating agent and naphthalene compound in the conventional manner. It has also been found that the stability of the alkylated product may be improved by filtration over activated charcoal and by alkali treatment to remove impurities, especially acidic by-products formed by oxidation during the course of the reaction. The alkali treatment is preferably carried out by filtration over a solid alkali material, preferably calcium carbonate (lime) . In a typical product work-up, it has been found, for example, that the RBOT (Rotating Bomb Oxidation Test) stability can be increased from a value of 184 minutes for an unstripped product (C 14 -alkylnaphthalene) to 290 minutes if the unreacted materials are removed by stripping and to 350 minutes if the stripped product is filtered over lime (CaC0 3 ) . Example 1 A commercially available catalyst containing 40 wt.% USY (Unit Cell Size = 244.5 nm (24.45 A)) in a clay and silica sol matrix was ammonium exchanged at room temperature by slurrying the catalyst with 5 vol/vol of 1 N NH 4 N0 3 for one hour. The catalyst was washed with water and then reexchanged and washed using the same procedure. This catalyst was then calcined for 5 hours in flowing air at a series of temperatures ranging from 350°C to 538°C to produce catalysts containing varying amounts of ammonia. The relative amounts of cation exchange sites in the ammonium and protonic form are shown below: Catalyst Calcination NH 4 + Cone. H + Cone. ID Temperature, • c (meq/g) (meq/g) A None 1.09 -0- B 350 0.85 0.24 C 375 0.64 0.45 D 400 0.59 0.50 E 425 0.54 0.55 F 450 0.34 0.75 G 538 -0- 1.09 The total ion exchange capacity of the catalyst as determined by temperature programmed ammonia desorption (Chester and Kerr method) is 1.09 meq/g. Example 2 In a series of six experiments, five parts of each of the catalysts of Example 1 were combined with ninety- five parts of naphthalene and 1-hexadecene in a 1:1.2 molar ratio in a stirred vessel. The contents of the vessel were then heated to 200°C and held at this temperature for four hours. The contents of the vessel were analyzed using gas chromatography to determine the amounts of unreacted naphthalene, olefin, monoalkylate and dialkylate. The results are summarized below: Naphthalene Hexadecene Monoalkylate Dialkylate Catalyst ID (wt.%) (wt.%) (wt.%) (wt.%) A 32.3 67.7 0 0 B 20.3 42.6 37.0 0 C 15.5 35.7 48.3 0.5 D 6.3 19.2 72.9 1.6 E 13.5 30.1 55.4 1.0 F 12.2 29.6 56.6 1.6 G 12.9 27.7 59.1 0.3 The above results show that Catalyst D, the catalyst with the ammonium cation concentration of 0.59 meq/g, is the most effective catalyst for this reaction. Only 54% of the exchangeable sites of this catalyst are in the ammonium form, the remainder are in the hydrogen form. This example demonstrates that only a fraction of the exchangeable sites need to contain a cation for the catalyst to be effective. Example 3 A commercially available USY with the properties shown below was combined with kaolin clay and a colloidal silica (Nalco) and spray dried at a temperature of 177°C (350°F) to produce a fluid catalyst containing 40 wt.% USY. UC Lattice Parameter, nm (A) 242.9 (24.29) Surface Area, m 2 /g 650 Sodium, ppm 445 Si0 2 , wt.% 85.8 A1 2 0 3 , wt.% 10.8 Si0 2 /Al 2 0 3 (molar) 13.8 Ash at 1000°C 98.7 Real Density, g/ml 2.384 Sorption Capacities' n_c 6 (P = 40 torr) 21.1 H 2 0 (p = 12 torr) 10.6 Surface area measured at P/P 0 = 0.03 ** Sorption Capacities are shown as wt ratios x 100 (= wt of sorbate x 100/wt of sorbate free zeolite) This catalyst was ion exchanged with ammonium nitrate using the procedure described in Example 1 and then calcined at 400"C in flowing air for five hours to produce Catalyst H. Another catalyst, Catalyst I, was prepared from the same base ammonium exchanged material by calcining at 538°C in flowing air for five hours. The ammonia content and water content of these catalysts were analyzed by TPAD and by determination of loss on ignition at 700°C. The results are summarized below: Calcination NH 4 + Cone, H + Cone, H 2 O Cone. Catalyst Temperature, °C (meq/g) (meq/g) (wt.%) ID H 400 0.04 0.06 2.0 I 538 -0- 0.10 0.1 Example 4 Five parts of each of the catalysts of Example 3 were combined with ninety-five parts of naphthalene and 1- hexadecene in a 1:1.2 molar ratio in a stirred vessel. The contents of the vessel were then heated to 200°C and held at this temperature for four hours. The contents of the vessel were analyzed using gas chromatography to determine the amounts of unreacted naphthalene, olefin, monoalkylate and dialkylate. The results are summarized below: Catalyst Naphthalene Hexadecene Monoalkylate Dialkylate ID (wt.%) (wt.%) (wt.%) (wt.%) H 3.1 8.3 79.7 8.9 I 4.9 5.9 63.0 26.2 The results show that only a small amount of ammonia (0.04 meq/g, 40% of the exchangeable sites) is necessary to modify the selectivity of the reaction and produce more of the highly desirable monoalkylate. Example 5 Five parts of Catalyst J, a commercially available rare earth containing USY (REUSY) catalyst having the properties shown below were combined with ninety-five parts of naphthalene and 1-hexadecene in a 1:1.2 molar ratio in a stirred vessel. Properties of the Catalyst Used in This Example RE 2 0 3 content, wt.% 1.0 Unit Cell Lattice Parameter, A 24.57 Ammonia Content, meq/g 0.56 Ash, wt.% (at 700°C) 89.5 The contents of the vessel were then heated to 200"C and held at this temperature for four hours. The contents of the vessel were analyzed using gas chromatography to determine the amounts of unreacted naphthalene, olefin, monoalkylate and dialkylate. The results are summarized below: Catalyst Naphthalene Hexadecene Monoalkylate Dialkylate ID (wt.%) (wt.%) (wt.%) (wt.%) J 2.5 13.6 82.1 1.8 Example 6 Five parts of Catalyst K, a commercially available rare earth containing USY (REUSY) catalyst having the properties shown below were combined with ninety-five parts of naphthalene and 1-hexadecene in a 1:1.2 molar ratio in a stirred vessel. Properties of the Catalyst Used in This Example RE 2 0 3 content, wt.% 3.0 Unit Cell Lattice Parameter, A 24.57 Ammonia Content, meq/g 0.50 Ash, wt.% (at 700°C) 80 The contents of the vessel were then heated to 200°C and held at this temperature for four hours. The contents of the vessel were analyzed using gas chromatography to determine the amounts.of unreacted naphthalene, olefin, monoalkylate and dialkylate. The results are summarized below: Catalyst Naphthalene Hexadecene Monoalkylate Dialkylate ID (wt.%) (wt.%) (wt.%) (wt.%) K 24.3 50.2 25.0 0.5 Comparison of the results of Examples 5 and 6 show that the rare earth content of the catalysts can affect yields and that the lower rare earth concentration (i.e., 1 wt.%) is preferred. The rare earth content of the preferred cataly-st (Example 5) catalyst would correspond to less than 15% of the total number of exchangeable sites. Example 7 Zeolite Y Crystals Six different samples of Zeolite Y crystals were used in this study to ascertain the effects of sodium level and framework Si0 2 /Al 2 0 3 ratio (or alternatively, Unit Cell Size, or UCS) . These samples had a somewhat smaller crystal size than other Y zeolite, from 0.2 to 0.4 μm v. 0.6 to 1.3 μm for typical Y zeolite. The samples were: HSZ-320NAA - Standard NaY zeolite (UCS = -246 nm (-24.64 A)) HSZ-320HOA - Partially NH 4 + exchanged and calcined NaHY HSZ-330NHA - Low sodium, ammonium form of USY (UCS = -245 nm (-24.50 A)) HSZ-330HSA - Low sodium, H-form of USY (UCS = -245 nm (24.50 A)) HSZ-330HUA - Low sodium, lower UCS H-form USY (UCS = -244 nm (-24.4 oA)) HSZ-360HUA - High silica USY, very low Na (UCS = -243 nm (-24.30 A)) Properties of as-received crystals are given in Table 1. Matrix The zeolites were incorporated into a silica-clay matrix at a 40 wt.% zeolite level. To produce this matrix, one part of colloidal silica (Nalco 1034A) was mixed with one part of a Thiele RC-32 clay, charged as a slurry. The zeolite was added to the clay-silica mixture and the formulation was spray dried at 177°C (350°F) , pH = 3 to 4.5 and then either calcined at 538°C (1000°F) or ammonium exchanged twice with 1 N NH 4 N0 3 solution, 5 volume of solution/volume catalyst, and then calcined as described below. Final Calcination The ammonium exchanged samples were calcined at either 572°F (300°C) or 752°F (400°C) to leave different levels of ammonia on the catalysts. The calcination consisted of heating the samples in flowing air (5 vol air/vol catalyst/min) from room temperature to the target temperature at 2.8°C/min (5°F/min) . The catalysts were then held at the final temperature in flowing air for 5 hours. The fully calcined samples (1000°F) were produced in a similar manner but were not ammonium exchanged prior to final calcination. Analysis of Reaction Products All alkylation runs were carried out in stirred flasks at 392°F (200°C). The runs consisted of charging the naphthalene and 1-hexadecene (in a 1:1.2 molar ratio) . The catalyst was then charged and the mixture was heated to the reaction temperature. Samples were taken at 2, 4, 6, and 8 hours and analyzed by gas chromatography (GC) . The amount of dimer was difficult to ascertain since it co-eluted with the monoalkylated naphthalene. In an attempt to deconvolute the amount of dimer and alkylated naphthalene, we calculated a predicted naphthalene and C 16 = Conversion based upon the analysis of the mono- and dialkylated naphthalenes. When the naphthalene conversion was higher than that measured from the naphthalene peak area, the excess was assumed to be dimer. This was the convention used to calculate the conversions shown in the tables below. TPAD Analysis Temperature programmed ammonia desorption (TPAD) was carried out using the method described by Kerr and Chester. Typically, the sample was heated in the DuPont Model 951 TGA from room temperature to 700°C at 10°C/minute under a 150 ml/minute flow of high purity helium. The stream of helium containing the desorbed ammonia was passed through c buffered solution where the excess base was titrated with sulfamic acid solution of known concentration (usually -0.017 g N/l) . The exchange capacity is reported as milliequivalents of ammonia per gram of catalyst (meq/g) based on the weight of the catalyst determined at 700°C. 400°C (752°F) Calcined Samples ZEOLITE Y SAMPLE 320NAA 320HOA 330HUA 3 33300HHSSAA 330NHA 360HUA Ash, wt.% 93.4 93.3 94.2 93.7 93.8 94.6 Na, wt.% (as-rec'd) 0.89 1.00 0.069 0.047 0.066 0.055 Na, wt.% (dry) 0.95 1.07 0.073 0.050 0.070 0.058 N, wt.% (as-rec'd) 0.46 0.55 0.21 0.50 0.61 0.11 N, wt.% (dry) 0.49 0.59 0.23 0.53 0.65 0.12 meq NH 3 /g Cat 1 0.35 0.42 0.16 0.38 0.46 0.086 meq Na/g Cat 0.41 0.47 0.03 0.02 0.03 0.02 10 meq NH 3 /g USY 2 0.875 1.05 0.40 0.95 1.15 0.215 meq Na/g USY 2 1.025 1.175 0.075 0.050 0.075 0.050 meq (Na+NH 3 )/g USY 2 1.90 2.23 0.475 1.00 1.23 0.265 As-Received Properties TPAD, meq NH 4 + /g CAT 0.25 0.34 0.10 0.30 0.28 0.04 y 00 1 15 TPAD, meq NH 4 + /g USY 2 0.625 0.85 0.25 0.75 0.70 0.10 Catalyst Exch. Capac, 0.89 0.18 0.38 0.52 0.10 (meq NH 4 + /g Cat) USY Exch. Capac, 2.23 0.45 0.95 1.30 0.25 20 (meq NH 4 7g USY) As-Rec'd NH 4 + as % 38 56 79 54 40 of Total Exch. Capac. Naphthalene Conv. 3 , % 98 96 83 89 87 95 Olefin (C 16 = ) Conv. 3 , % 84 82 72 77 78 87 25 Dialkylnaph. Select. 3 , % 2 3 5 4 7 10 Computed occupancies 4 , vol.% + Notes: Ammonia content based on elemental analysis of nitrogen on the catalyst Assumes that catalyst contains 40 wt.% USY 8 hours on stream, 200°C, Naphthalene:C 16 ==1:1.2 (molar), 5 wt.% catalyst Na is assumed to be in sodalite cages following calcination and ammonium exchange. I 538°C (1000°F) Calcined Samples Zeolite Y Sample 320NAA 320HOA 330HUA 330HSA 330NHA 360HUA Ash, wt.% 96.6 96.8 95.6 95.4 97.6 98.1 Na, wt.% (as-rec'd) 3.55 4.30 0.145 0.147 0.157 0.132 Na, wt.% (dry) 3.68 4.44 0.152 0.154 0.160 0.134 meq Na/g Cat 1.60 1.93 0.066 0.066 0.069 0.058 meq Na/g USY 4.00 4.83 0.165 0.165 0.173 0.145 Wt.% USY (XRD) 42 33 42 42 41 40 meq Na/g USY (XRD) 3.80 5.84 0.157 0.160 0.171 0.146 10 Unit Cell Parameter, A 24.60 24.60 24.34 24.44 24.44 24.26 Al/(Si+Al) 0.214 0.214 0.0606 0.1196 0.1196 0.0134 g Theo. Exch. Capac 1 4.58 4.58 1.06 2.08 2.08 0.233 ' (meq Na/g USY) As-Rec'd Na as % 83 105 15.6 7.7 8.2 62.7 15 of Total Exch. Capac. Naphthalene Conv. 2 ,% 34 40 81 83 85 92 Olefin (C 16 = ) Conv. 2 ,% 28 34 82 85 86 92 Dialkylnaph. Select. 2 ,% 0 0 21 23 22 21 Notes: 20 1 Computed; Al/(A1+Si) = 0.59 a 0 (A) - 14.3 2 8 hours on stream, 210°C, Naphthalene:C 16 = = 1:1.2 (molar), 5 wt.% catalyst. These data show it is essential for optimum performance to have both ammonium and protonic cations on the exchangeable sites. It is also beneficial to have some rare earths, and some water, but the amount of water found in most commercial grade naphthalene supplies (typically 0.75 wt %) is enough.

Claims: WE CLAIM : 1. A process for preparing long chain alkyl substituted naphthalenes which comprises alkylating a naphthalene with an alkylating agent possessing an alkylating aliphatic group having at least six carbon atoms under alkylation reaction conditions in the presence of an alkylation catalyst comprising a porous crystalline zeolite containing exchangeable sites and both ammonium and protonic species associated with the exchangeable sites, and wherein the ratio of ammonium:protonic species is within the range of 95:5 to 5:95, molar basis, to form an alkylated naphthalene possessing at least one alkyl group derived from the alkylating agent. 2. The process of Claim 1 wherein the zeolite is a large pore size zeolite having pores with a minimum dimension of at least 74 nm. 3. The process of Claim 1 wherein the zeolite has a Constraint Index of not more than 2. 4. A process according to Claim 3 wherein the zeolite has a Constraint Index of not more than 1. 5. The process of Claim 1 wherein the zeolite comprises zeolite X or zeolite Y. 6. The process of Claim 5 wherein the zeolite is USY. 7. The process of Claim 1 wherein the ratio of ammonium: protonic species is 90:10 to 10:90. 8. The process of Claim 1 wherein the ratio of ammonium: protonic species is 65:35 to 35:65. 9. The process of Claim wherein the ratio of ammonium: protonic species is about 40:60 to 50:50. 10. The process of Claim 1 wherein the zeolite is ammonium exchanged USY calcined to convert from 45 to 60 % of the ammonium form to the protonic form. 11. The process of Claim 1 wherein the alkylating aliphatic group contains at least 8 carbon atoms. 12. The process of Claim 11 wherein the alkylating aliphatic group contains at least 12 carbon atoms. 13. The process of Claim 12 wherein the alkylating aliphatic group contains from 14 to 20 carbon atoms. 14. The process of Claim 1 wherein the alkylating agent comprises an olefin. 15. The process of Claim 1 wherein the alkylation reaction conditions include a temperature of 100"C to 400°C, pressure of 20 to 2532 kPa, a WHSV of 0.1 to 10 and an alkylatable aromatic:alkylating agent mole ratio of 0.1:1 to 50:1. 16. The process of Claim 15 wherein alkylation reaction conditions include a temperature of 100°C to 300°C, a pressure of 101 to 506 kPa, a WHSV of 0.5 to 5 and an alkylatable aromatic:alkylating agent mole ratio of 0.5:1 to 5:1. 17. A process for preparing long chain alkyl substituted naphthalenes comprising alkylating naphthalene with an olefin containing at least 8 carbon atoms under alkylation reaction conditions in the presence of an alkylation catalyst comprising an ultrastable Y zeolite with exchangeable sites containing both ammonium and protonic species at a molar ratio of ammonium:protonic species from 65:35 to 35:65, to form an alkylated naphthalene. 18. The process of Claim 17 wherein the ratio of ammonium:protonic species is about 46 to 54. 19. The process of claim 17 wherein the catalyst is prepared by essentially complete ammonium exchange of the zeolite followed by calcination at 300 to 400°C for a time sufficient to remove from 45 to 65 % of the ammonia. 20. The process of claim 19 wherein the catalyst is calcined at 400"C to produce a catalyst with 46 % ammonium and 54 % protonic species.

Inventors: ARDITO SUSAN CHMURA, ASHJIAN HENRY, DEGNAN THOMAS F, HELTON TERRY EUGENE, LE QUANG NGOC, QUINONES AUGUSTO RODOLFO, ARDITO, SUSAN, CHMURA, ASHJIAN, HENRY, DEGNAN, THOMAS, F., HELTON, TERRY, EUGENE, LE, QUANG, NGOC, QUINONES, AUGUSTO, RODOLFO
Applicants: MOBIL OIL CORP, MOBIL OIL CORPORATION
Application year: 1994
Main classification: C07C2
IPC codes: B01J29, B01J37, C07B61, C07C2, C07C15